EP4228790A1 - Procédé et appareil pour la désulfuration d'un mélange gazeux acide - Google Patents

Procédé et appareil pour la désulfuration d'un mélange gazeux acide

Info

Publication number
EP4228790A1
EP4228790A1 EP21793855.4A EP21793855A EP4228790A1 EP 4228790 A1 EP4228790 A1 EP 4228790A1 EP 21793855 A EP21793855 A EP 21793855A EP 4228790 A1 EP4228790 A1 EP 4228790A1
Authority
EP
European Patent Office
Prior art keywords
mode
stream
gas mixture
free
sour gas
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
EP21793855.4A
Other languages
German (de)
English (en)
Inventor
Bernhard Schreiner
Mika Tuuva
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Publication of EP4228790A1 publication Critical patent/EP4228790A1/fr
Pending legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00—Sulfur; Compounds thereof
    • C01B17/02—Preparation of sulfur; Purification
    • C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
    • C01B17/0404—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds

Definitions

  • the present invention relates to a method for the desulphurisation of a sour gas mixture and to corresponding apparatus according to the precharacterising clauses of the independent claims.
  • the Claus process originally only mixed hydrogen sulphide or a corresponding sour gas mixture with oxygen and passed the mixture across a pre-heated catalyst bed. It was later modified to include a free-flame oxidation upstream the catalyst bed in a so- called Claus furnace. Most of the sulphur recovery units (SRU) in use today operate on the basis of a correspondingly modified process. If, in the following, therefore, shorthand reference is made to a “Claus process” or to a corresponding apparatus, this is intended to refer to a free-flame modified Claus process as just described.
  • oxygen enrichment is a well-known economic and reliable method of debottlenecking existing Claus sulphur recovery units with minimal capital investment.
  • Oxygen enrichment is, however, as described in detail below, not limited to retrofitting existing Claus sulphur recovery units but can likewise be advantageous in newly designed plants.
  • the “term oxygen enrichment” shall, in the following, refer to any method wherein, in a Claus sulphur recovery unit or in a corresponding method, at least a part of the air introduced into the Claus furnace is substituted by oxygen or a by gas mixture which is, as compared to ambient air, enriched in oxygen or, more generally, has a higher oxygen content than ambient air.
  • Oxygen or oxygen enriched gas mixtures for Claus sulphur recovery units can be, in general, provided by cryogenic air separation methods and corresponding air separation units (ASU) as known from the prior art, see e.g. Haering, H.-W., “Industrial Gases Processing,” Wiley-VCH, 2008, especially chapter 2.2.5, “Cryogenic Rectification.”
  • Cryogenic air separation units typically comprise a so-called warm section configured for compression, pre-cooling, drying and pre-purification of feed air, and a so-called cold section configured for heat exchange and rectification.
  • An object of the present invention is to provide an improved operation of a Claus process or a corresponding Claus sulphur recovery unit under turn-down conditions, as further described hereinbelow.
  • the present invention provides a method for the desulphurisation of a sour gas mixture and a corresponding apparatus comprising the features of the independent claims, respectively.
  • Preferred embodiments are subject of the dependent claims and of the description below.
  • the sour gas mixture may, in the present invention, particularly be obtained from a gas mixture containing hydrogen sulphide and optionally carbon dioxide and other sour gases, especially in a chemical and/or physical absorption step using an absorption liquid, particularly in a so-called amine unit.
  • Obtaining a sour gas mixture can also form part of the invention.
  • the desulphurisation is performed, according to the invention, in the form of a Claus process including free-flame oxidation or a variant thereof as described at the outset.
  • the term “desulphurisation” as used herein shall refer to any process including conversion of a first sulphur compound comprising sulphur at a lower oxidation stage, which is contained in a sour gas mixture, to a second sulphur compound comprising sulphur at a higher oxidation stage in a first reaction step, and particularly further including forming elementary sulphur from the second sulphur compound in a second reaction step, the elementary sulphur particularly being obtained in liquid state.
  • the first sulphur compound may be hydrogen sulphide and the second sulphur compound may be sulphur dioxide.
  • the first reaction step may particularly include combusting the first sulphur compound and the second reaction step may particularly include using a suitable catalysis reaction as generally known for the Claus process.
  • a mixture of components may be rich or poor in one or more components, where the term “rich” may stand for a content of more than 75%, 80%, 85%, 90%, 95%, 99%, 99.5% or 99.9% and the term “poor” for a content of less than 25%, 20%, 15%, 10%, 5%, 1%, 0.5% or 0.1%, on a molar, weight or volume basis.
  • a sour gas mixture with a hydrogen sulphide content of more than 80% is generally referred to as “rich” while a sour gas mixture containing less hydrogen sulphide is generally referred to as “lean.”
  • a mixture may also be, in the language as used herein, enriched or depleted in one or more components, especially when compared to another mixture, where “enriched” may stand for at least 1 , 5 times, 2 times, 3 times, 5 times, 10 times or 100 times of the content in the other mixture and “depleted” for at most 0.75 times, 0.5 times, 0.25 times, 0.1 times, or 0.01 times of the content in the other mixture.
  • pressure level and “temperature level” are used herein in order to express that no exact pressures but pressure ranges must be used in order to realise the present invention and advantageous embodiments thereof. Different pressure and temperature levels may lie in distinctive ranges or in ranges overlapping each other. They also cover expected and unexpected, particularly unintentional, pressure or temperature changes, e.g. inevitable pressure or temperature losses. Values expressed for pressure levels in bar units are absolute pressure values.
  • sour gas mixture refers, in the language as used herein, to a gas mixture containing at least hydrogen sulphide and optionally carbon dioxide and other known sour gases in an amount of at least 50%, 75%, 80% or 90% by volume, these numbers relating to the content of one of these compounds or to a common content of several ones. Further components besides sour gases may be present in a sour gas mixture as well, particularly water, hydrocarbons, benzene, toluene and xylenes (BTX), carbon monoxide, hydrogen, ammonia and mercaptans.
  • BTX benzene, toluene and xylenes
  • a sour gas mixture used as a feed for a Claus sulphur recovery unit usually originates from a sour gas sweetening plant, e.g. for sweetening natural gas or a gas from a petrochemical or oil refinery plant.
  • the sour gas mixture containing varying amounts of hydrogen sulphide and carbon dioxide, is saturated with water and frequently also contains small amounts of hydrocarbons and other impurities in addition to the principal components.
  • the sour gas mixture enters a typical Claus sulphur recovery unit at about 0.5 to 1 .0 barg or about 0.8 to 1.3 barg and a temperature between ambient and up to about 200 °C, if preheat measures are taken, like eg heat exchange with steam .
  • Claus sulphur recovery units In classical Claus sulphur recovery units, combustion air is compressed to an equivalent pressure by centrifugal blowers. Both inlet streams then flow to a burner which fires into the Claus furnace.
  • a sour gas mixture used as a feed for a Claus sulphur recovery unit may be combined with a second stream of so-called sour water stripper gas containing hydrogen sulphide and major amounts of ammonia. It is possible to increase the Claus furnace temperature by so-called co-firing, i.e. sending fuel - typically hydrocarbons and/or hydrogen - as an additional feed stream into the furnace chamber, either directly through a dedicated nozzle or by admixing to the main sour gas feed stream.
  • the gas mixture from the Claus furnace at a temperature of typically 900 °C and up to 1 ,450 °C, is typically cooled while generating high-pressure steam in a waste heat boiler and further cooled while producing low-pressure steam in a separate heat exchanger.
  • This cools the hot gases to approximately 160 °C, condensing most of the sulphur which has already formed up to this point.
  • the resultant liquid sulphur is removed in a separator section of the condenser and flows by gravity to a sulphur storage tank. Here it is kept molten, at approximately 140 °C, by steam coils. Sulphur accumulated in this reservoir is either formed to solid particles by cooling or pumped to trucks or rail cars for shipment.
  • a typical Claus sulphur recovery unit comprises one free-flame reaction stage, i.e. one furnace, and two or three catalytic reaction stages. Each reaction step converts a smaller fraction of the remaining sulphur gases to sulphur vapour.
  • TGTU tail gas treatment unit
  • Wet scrubbing processes may include a frontend section to convert all of the sulphur compounds still contained in the tail gas back into hydrogen sulphide.
  • the hydrogen sulphide-containing tail gas is contacted with a solvent to remove the hydrogen sulphide, much like in a conventional gas treating plant. The solvent is then regenerated to strip out the hydrogen sulphide, which is then recycled to the thermal stage of the upstream Claus sulphur removal unit for subsequent conversion and recovery.
  • So-called oxygen enrichment is, as mentioned, a well-known economic and reliable method of debottlenecking existing Claus sulphur recovery units with minimal capital investment. It can also eliminate the need for fuel gas co-firing in the reaction furnace, required to maintain an adequate temperature for sufficient contaminant destruction, for example for destruction of benzene, toluene and xylenes (BTX) in the sour gas mixture. Generally, a minimum temperature is required to maintain a stable flame (above about 900 °C) and even higher temperatures of about 1 ,250 °C or higher are required to destroy ammonia (present in sour gas mixtures obtained in refineries).
  • Whether or not a corresponding co-firing is required particularly depends on the hydrogen sulphide content of the sour gas mixture treated and whether a sufficient temperature and a stable flame can be obtained by burning the sour gas mixture alone.
  • the concept of oxygen enrichment entails replacing part of the air fed to the Claus furnace by oxygen-enriched air or pure oxygen.
  • the temperature within the Claus combustion chamber rises and volumetric flow through the Claus sulphur recovery unit decreases, allowing more of the sour gas mixture to be fed to the system. This results in an increased sulphur production capacity without the need for significant modifications to existing equipment or major changes to the process plant pressure profile.
  • oxygen enrichment is not limited to retrofitting or debottlenecking existing Claus sulphur recovery units, but can also have advantages in newly designed plants, e.g. where the acid gas mixtures fed are lean and contain benzene, toluene and xylenes.
  • Such plants classically require feed gas and/or combustion air preheating and the use of fuel gas co-firing and have not, historically, been considered for oxygen enriched operation.
  • the use of oxygen enriched technology results in a reduction in the physical size of all major equipment items and an associated, significant reduction in capital cost.
  • a large reduction in fuel requirements in co-firing in the Claus furnace and other units can be achieved and therefore more fuel, e.g. natural gas, can be used for other purposes or provided as a product of the whole plant.
  • a particular advantage of oxygen enrichment is, furthermore, that the tail gas downstream a tail gas treatment unit is less “diluted” with nitrogen from the combustion air classically used. If little or no additional nitrogen is introduced into the process, the main component of the sour gas mixture after desulphurisation, i.e. carbon dioxide, and other components like hydrogen can be recovered in a simpler and more cost-effective way, e.g. by cryogenic technology alone and without energy-intensive wet technology.
  • low level oxygen enrichment is generally used in the field for cases in which less than 28 vol.-% of oxygen are present in the free-flame oxydation, as e.g. mentioned in A.L. Kohl and R.B. Nielsen, “Gas Purification”, 5th Edition, Gulf Publishing, Houston, Texas, DOI: 10.1016/B978-088415220-0/50008-2, particularly chapter 8, “Sulfur Recovery Processes”.
  • technical oxygen is injected into a supply line providing combustion air to the free-flame oxydation step of a Claus process.
  • Claus plants originally adapted to be operated without oxygen enrichment may be adapted to implement some degree of oxygen enrichment (“revamp”) in the form of low-level oxygen enrichment particularly easily.
  • oxygen accounts for more than 28 % by volume of process air, additional measures have to be taken, according to the conventional view also expressed in documents such as EP 3 276 262 A1 , to introduce the oxygen into the Claus process.
  • oxygen is conventionally fed into the Claus furnace by one or more separate oxygen lances up to a concentration of about 45 vol.-%.
  • the oxygen can be fed by oxygen lances combined with process characteristics like staged combustion or process gas recycle. The latter correspond to the so-called “high-level” oxygen enrichment mode.
  • the present invention is of used in connection with sour gas desulphurisation involving the Claus process.
  • Co-firing is frequently applied, and typically applied in cases where other measures, like e.g. preheating of feed gas, are non-sufficient or not possible.
  • Co-firing is regarded as a measure of last resort, because it causes unwanted effects like e.g. increased carbon sulphide concentrations in the Claus process gas (potentially increasing sulphur dioxide emissions).
  • the major disadvantage of co-firing from an operational point of view is due to non-complete combustion of co-fired hydrocarbons leading to soot particles in the process gas. The latter particles precipitate as solids and thereby lead to negative effects in the Claus sections down-stream the Claus furnace:
  • oxygen enrichment was typically not applied because the significantly reduced overall gas flow combined with higher flame velocity jeopardizes the mechanical integrity of the (tip of the) main Claus burner; i.e. when the open flame is located and burning too near to the material of the burner.
  • oxygen enrichment and co-firing are combined at low load operational conditions.
  • This combination allows for reaching targeted Claus furnace temperature levels (e.g. 1 ,250 °C, as commonly seen as minimum for sufficient ammonia destruction) with significantly less fuel amount application as compared with co-firing alone and therefore also comparably reduced build-up of soot and carbon sulphides, as carbon disulfide in particular.
  • a method for the desulphurisation of a sour gas mixture wherein the sour gas mixture is subjected to a free- flame oxidation producing a process gas containing sulphur dioxide, and wherein the process gas is at least in part subjected to a catalytic conversion converting the sulphur dioxide at least in part to elementary sulphur, the sour gas mixture being subjected to the free-flame oxidation in a first amount per time unit in a first mode of operation and in a second amount per time unit not exceeding a third of the first amount per time unit in a second mode of operation, and the free-flame oxidation being performed using an oxydant stream with an oxygen content exceeding that of atmospheric air in the first mode of operation.
  • the second amount per time unit can e.g. be in the range from 10 to 30 percent of the first amount per time unit. Be it understood that the time units referred to for the first and the second modes of operation are the same, the “amounts per time unit” e.g. being standard cubic meters.
  • the free-flame oxidation is performed using the oxydant stream with the oxygen content exceeding that of atmospheric air (also) in the second mode of operation, and heat is supplied by combusting a fuel stream other than the sour gas mixture (i.e. typically hydrocarbons or hydrogen) in the second mode of operation. That is, in the second mode of operation, both an oxygen enrichment and co-firing are applied, resulting in the advantages as mentioned before.
  • the fuel stream other than the sour gas mixture may be e.g. natural gas from which the sour gas mixture is formed.
  • the oxydant stream may be pure oxygen or it may comprise at least 21 , 25, 30, 40, 50, 60, 70, 80 or 90% of oxygen, particularly by volume. That is, the oxydant stream may be “technical” oxygen or any other stream enriched in oxygen as compared to atmospheric air. It may particularly provided using an air separation unit as mentioned.
  • An oxygen-enrichment is generally present if a stream containing more than 20.9 vol% (which is the oxygen concentration in dry ambient air) is present.
  • oxygen is provided to be present in the free-flame oxidation at a concentration not exceeding 28%. That is, the present invention is particularly used in connection with low level oxygen enhancement, as explained in more detail above.
  • the oxydant stream may be used in a first amount per time unit (according to the definition above) in the first mode of operation and in a second amount per time unit in the second mode of operation, the second amount per time unit not exceeding 50% of the first amount per time unit.
  • no or less heat is supplied by combusting the fuel stream in the first mode of operation as compared to the second mode of operation.
  • co-firing is reduced or omitted in order to avoid the problems mentioned above.
  • a temperature level of a gas stream formed in the free-flame oxidation is in the range from 1 ,000 to 1 ,500 °C, particularly above 1 ,250 °C as often the case in refineries, in order to provide for the destruction of ammonia, as mentioned.
  • the sour gas mixture may be formed using at least one sour gas separated from natural gas or at least one sour gas separated from product stream(s) from oil refining operations, and the second mode of operation is a turndown mode of operation, in which the sour gas mixture may be available in a smaller amount, e.g. due to the fact that a sweetening plant operates at reduced capacity.
  • the present invention is used in connection with a Claus process, i.e. the free-flame oxidation and the catalytic conversion may be performed in process units of a process arrangement adapted to perform a Claus process.
  • the present invention also relates to an apparatus for performing a gas treatment method as set forth in the corresponding independent apparatus claim, which is not recited herein for reasons of conciseness.
  • Such an apparatus may particularly include a control unit programmed or adapted to control the units of the apparatus particularly in a turn-down mode as described.
  • Figure 1 schematically illustrates a gas treatment method including an oxidative process for desulphurisation of a sour gas mixture in general.
  • Figure 2 schematically illustrates a method for the desulphurisation of a sour gas mixture according to an embodiment of the present invention.
  • Figure 1 schematically illustrates a gas treatment method including an oxidative process 4 for desulphurisation of a sour gas mixture in general.
  • the process is illustrated as using a gas from an air separation process and is further illustrated to include a Claus process as the oxidative process 4.
  • a sour natural gas stream a from a gas field 1 or a gas mixture from oil refining operations containing hydrogen sulphide is introduced into a sour gas removal unit 2, in this particular case including an amine unit 21 as mentioned before.
  • the amine unit 21 is operated as generally known in the art, in the present example using a steam stream b which is used to heat a reboiler in the amine unit 21 (not shown).
  • a steam stream c of a lower temperature or a condensate stream c can be formed.
  • a sweetened gas stream d is withdrawn from the sour gas removal unit 2 and optionally subjected to further treatment 3, providing a further treated gas stream e which can e.g. fed into a gas pipeline.
  • a sour gas stream f is also withdrawn from the sour gas removal unit 2 and is introduced into the oxidative process 4 which is embodied as a Claus process 4, or, more specifically, into a Claus furnace 41 in the Claus process 4.
  • Additional gas streams may be supplied to the Claus process 4, which e.g. may be generated by a sour water stripping unit as often the case in refineries and coming with significant amounts of ammonia in the gas matrix.
  • a part of the sour gas stream f can also be reinjected into the gas field 1 , as indicated by a dotted arrow in Figure 1 .
  • a sulphur stream g is withdrawn from the Claus process 4 and is subjected to a sulphur product handling 5. From this, a sulphur product stream h is withdrawn or otherwise provided.
  • a tail gas stream i also withdrawn from the Claus process 4 is treated in a manner known per se.
  • the tail gas treatment unit 6 provides a purified stack gas stream k with little or no sulphur compounds. Components from the tail gas treatment unit 6 can also, as illustrated with a dashed arrow, be reintroduced into the Claus process 4 or its Claus furnace 41 .
  • the tail gas treatment unit 6 may also comprise a unit operable by heat, e.g. an amine unit 61 , wherein the heat is provided in the form of steam.
  • a steam stream o is provided to this unit and a steam stream p of a lower temperature or a condensate stream p can be formed.
  • One or both of the amine unit 21 in the sour gas removal unit 2 and the unit 61 in the tail gas treatment unit 6 may be provided and/or one or both of them may be operated using steam.
  • the Claus process 4 is operated with an oxygen-containing gas stream as oxidant which is either air only or air supplemented respectively substituted by technically generated oxygen, i.e. using oxygen enrichment, in a regular operation mode. Therefore, using respective oxygen sources 7, an oxygen-containing gas, i.e. an oxygen stream or an oxygen-enriched stream I which can be combined with an air stream from an air blower (referred to as “oxydant stream hereinbefore”) is provided which is also introduced into the Claus process 4 or its furnace 41 .
  • the oxygen source 7 can be a pipeline from a central supply grid, a dedicated oxygen production unit such as a cryogenic air separation unit or a vacuum pressure swing adsorption (VPSA) installation may be based on a tank installation filled with liquified oxygen combined with a subsequent vaporizer unit.
  • stream I may either be provided to the furnace 41 separately from an air stream r, such as from an air blower (not shown) or may be admixed thereto, as shown in the form of a solid arrow. While the former is typical for so-called mid or high level oxygen enrichment (in which oxygen contents of more than 28% are used), the latter is typically performed in the case of so-called low level oxygen enrichment and particularly perfomed in the case of the present invention.
  • a fuel gas stream q can also be supplied to the Claus process 4 or more precisely its furnace 41.
  • a control unit 10 is adapted to provide control instructions.
  • Figure 2 schematically illustrates a method 100 for the desulphurisation of a sour gas mixture according to an embodiment of the present invention.
  • a first mode of operation is performed which is an operation mode in which a corresponding apparatus is run at full or design capacity.
  • a second mode of operation is performed which is an operation mode in which a corresponding apparatus is run in a turn-down mode at reduced capacity.
  • a sour gas mixture is subjected to a free-flame oxidation producing a process gas containing sulphur dioxide, and the process gas is at least in part subjected to a catalytic conversion converting the sulphur dioxide at least in part to elementary sulphur.
  • the sour gas mixture is subjected to the free-flame oxidation in a first amount per time unit in a first mode of operation and in the second mode of operation, i.e. the method step 130, the sour gas mixture is subjected to the free-flame oxidation in a second amount per time unit not exceeding a third of the first amount per time unit.
  • the free-flame oxidation is performed using an oxydant stream with an oxygen content exceeding that of atmospheric air, and in the second method step 130, heat is supplied by combusting a fuel stream other than the sour gas mixture in the second mode of operation.
  • a switching between the first and second operation modes performed in method steps 110 and 130 is initiated.
  • a fuel stream is started to be provided and that particularly an amount per time unit of the oxydant stream is reduced.
  • a switching back to the first and operation mode may be performed, wherein the measures mentioned are reverted.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Environmental & Geological Engineering (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Inorganic Chemistry (AREA)
  • Treating Waste Gases (AREA)

Abstract

L'invention concerne un procédé (100) pour la désulfuration d'un mélange gazeux acide, le mélange gazeux acide étant soumis à une oxydation à flamme libre produisant un gaz de traitement contenant du dioxyde de soufre, et le gaz de traitement étant au moins en partie soumis à une conversion catalytique convertissant le dioxyde de soufre au moins en partie en soufre élémentaire, le mélange gazeux acide étant soumis à l'oxydation à flamme libre dans une première quantité par unité de temps dans un premier mode de fonctionnement et dans une seconde quantité par unité de temps ne dépassant pas un tiers de la première quantité par unité de temps dans un second mode de fonctionnement, et l'oxydation à flamme libre étant effectuée à l'aide d'un courant oxydant ayant une teneur en oxygène supérieure à celle de l'air atmosphérique dans le premier mode de fonctionnement. L'oxydation à flamme libre est effectuée à l'aide du flux oxydant avec la teneur en oxygène supérieure à celle de l'air atmosphérique dans le second mode de fonctionnement, et de la chaleur est fournie par combustion d'un flux de combustible autre que le mélange gazeux acide dans le second mode de fonctionnement. Un appareil correspondant fait également partie de l'invention.
EP21793855.4A 2020-10-13 2021-10-12 Procédé et appareil pour la désulfuration d'un mélange gazeux acide Pending EP4228790A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP20020472.5A EP3984621A1 (fr) 2020-10-13 2020-10-13 Procédé et appareil de désulfuration d'un mélange de gaz impur
PCT/EP2021/025399 WO2022078628A1 (fr) 2020-10-13 2021-10-12 Procédé et appareil pour la désulfuration d'un mélange gazeux acide

Publications (1)

Publication Number Publication Date
EP4228790A1 true EP4228790A1 (fr) 2023-08-23

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EP20020472.5A Withdrawn EP3984621A1 (fr) 2020-10-13 2020-10-13 Procédé et appareil de désulfuration d'un mélange de gaz impur
EP21793855.4A Pending EP4228790A1 (fr) 2020-10-13 2021-10-12 Procédé et appareil pour la désulfuration d'un mélange gazeux acide

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EP20020472.5A Withdrawn EP3984621A1 (fr) 2020-10-13 2020-10-13 Procédé et appareil de désulfuration d'un mélange de gaz impur

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Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1989012023A1 (fr) * 1988-06-08 1989-12-14 American Combustion, Inc. Procede et appareil de recuperation de soufre a partir de gaz contenant du sulfure d'hydrogene
EP3276262A1 (fr) 2016-07-29 2018-01-31 Linde Aktiengesellschaft Procédé de fonctionnement d'un brûleur de claus
WO2019081065A1 (fr) * 2017-10-24 2019-05-02 Linde Aktiengesellschaft Procédé et appareil de traitement d'un mélange de gaz acides
WO2019120619A1 (fr) * 2017-12-19 2019-06-27 Linde Aktiengesellschaft Procédé de traitement de gaz comprenant un processus oxydatif fournissant de la chaleur perdue et appareil correspondant
WO2020160842A1 (fr) * 2019-02-07 2020-08-13 Linde Gmbh Procédé et appareil de traitement de gaz comprenant un processus oxydatif pour traiter un mélange de gaz acides à l'aide de gaz provenant d'un processus de séparation d'air

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EP3984621A1 (fr) 2022-04-20

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